EP0642601B1 - Dual-directional flow membrane support for water electrolyzers - Google Patents

Dual-directional flow membrane support for water electrolyzers Download PDF

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Publication number
EP0642601B1
EP0642601B1 EP93914147A EP93914147A EP0642601B1 EP 0642601 B1 EP0642601 B1 EP 0642601B1 EP 93914147 A EP93914147 A EP 93914147A EP 93914147 A EP93914147 A EP 93914147A EP 0642601 B1 EP0642601 B1 EP 0642601B1
Authority
EP
European Patent Office
Prior art keywords
water
porous sheet
electrolyzer
ion exchange
exchange membrane
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP93914147A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0642601A1 (en
Inventor
Hugh A. Carlson
Andrei Leonida
James F. Mcelroy
Eric M. Shane
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Raytheon Technologies Corp
Original Assignee
United Technologies Corp
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Application filed by United Technologies Corp filed Critical United Technologies Corp
Publication of EP0642601A1 publication Critical patent/EP0642601A1/en
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    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
    • C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
    • C25B9/23—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms comprising ion-exchange membranes in or on which electrode material is embedded
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/70—Assemblies comprising two or more cells
    • C25B9/73—Assemblies comprising two or more cells of the filter-press type
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

Definitions

  • the present invention relates to water electrolyzers, and especially to water electrolyzers which can operate under high pressure gradients.
  • Ion exchange membrane water electrolyzers for producing hydrogen and oxygen from water have been known for more than 20 years.
  • the electrolyzer's components typically include chambers for the introduction of water and the removal of hydrogen, oxygen, and water, an ion exchange membrane disposed between catalyst electrodes, and metal screens which support the ion exchange membrane and form the chambers.
  • a first metal screen set 1 which forms the anode chamber is located above the catalytic anode electrode 7 which intimately contacts the ion exchange membrane 5 .
  • the opposite side of the ion exchange membrane 5 intimately contacts a catalytic cathode electrode 9 , which lies above a second metal screen set 3 which forms the cathode chamber.
  • the metal screens of the water electrolyzer perform numerous functions. Generally, a low pressure gradient is permitted across the ion exchange membrane within the electrolyzer in order to simplify the system pressure controls. Often, up to about 1.38MPa (200 per square inch (psi)) of pressure exists across the ion exchange membrane during electrolyzer operation. Since the ion exchange membrane possesses low structural integrity, the pressure gradient across the ion change membrane can cause failure thereof. Therefore, the natal screens are used to provide structural support to the ion exchange membrane during operation. These metal screens also form flow paths for the water, oxygen, and hydrogen, and they conduct electrons utilized during the water electrolysis to and from the electrodes, into adjacent cells, or to external circuits.
  • the present invention relates to a water electrolyzer.
  • This water electrolyzer comprises an anode electrode, an anode chamber formed by a first screen set superimposed on said anode electrode, a cathode electrode, a cathode chamber formed by a second screen set superimposed on said cathode electrode, an ion exchange membrane disposed between and in intimate contact with said anode electrode and said cathode electrode, and a porous sheet interposed between and in intimate contact with the first screen set and the anode electrode said porous sheet having several pore sizes of which the small sizes allow the access of electrolyte only whereas the larger pores permit the removal of the gas bubbles from the electrode surface.
  • the present invention further relates to a method for electrolyzing water using a water electrolyzer.
  • This method includes introducing water to the anode chamber of the electrolyzer. The water passes through pores to the said sheet to the anode electrode where it is electrolyzed to oxygen and hydrogen ions.
  • the hydrogen ions migrate across the ion exchange membrane to the cathode electrode where they form molecular hydrogen. This molecular hydrogen exits the electrolyzer through the cathode chamber while the oxygen exits the electrolyzer by passing through the pores of the sheet and then out through the anode chamber.
  • Figure 1 is an illustration of a basic prior art ion exchange membrane water electrolyzer.
  • Figure 2 is an illustration of a basic prior art ion exchange membrane water electrolyzer and the flow path through this electrolyzer.
  • Figure 3 is a water electrolyzer which uses metal screen set to form the anode and the cathode chambers and further uses a fine mesh screen to provide additional support for the ion exchange membrane.
  • Figure 4 is one embodiment of the water electrolyzer of the present invention using metal screen sets to form the anode and cathode chambers with a porous sheet located between the anode chamber and the anode electrode.
  • Figure 5 is a graph of the water electrolyzer performance which was realized using various supports including the prior art metal screen, the fine mesh screen; and finally the porous sheet of the present invention.
  • the present invention relates to a water electrolyzer capable of operating at ion exchange membrane pressure gradients up to about 13.8 MPa (2000 psi) and greater.
  • the electrolyzer components include metal screens, a porous sheet, an anode electrode, an ion exchange membrane, and a cathode electrode.
  • the ion exchange membrane requires additional support to avoid extruding into the metal screens.
  • the additional ion exchange membrane support can be provided by employing fine mesh screens and/or porous sheets.
  • the fine mesh screens should be electrically conductive, and therefore are generaily metal screens having a mesh size of about 5/0 to about 6/0. Additionally, these fine mesh screens are capable of providing structural integrity to the ion exchange membrane at pressure differentials exceeding about 1.38 MPa (200 psi), and typically up to about 6,89 MPa (1000 psi) or greater.
  • Some possible fine mesh screens include titanium, zirconium, tantalum, and niobium expanded metal screens produced by X-MET Corporation, Bridgeport, Connecticut, among others. These fine mesh screens typically have a thickness of about 0.05 millimeters (mm) to about 0.3 mm. Although thicker fine mesh screens are feasible, they are impractical due to decreased mass transfer rates in these thicker screens.
  • porous sheets as shown in Figure 4, which is meant to be exemplary, not limiting, oxygen produced at the anode electrode 7 escapes through the pores of the porous sheet 14 while additional water flows to the anode electrode 7 for electrolysis.
  • the porous sheet 14 is perforated having multiple-pore sizes. Water wicks from the metal screen set 1 , through the porous sheet 14 , to the anode electrode 7 . on the anode electrode 7 , electrolysis converts the water to oxygen and hydrogen ions. This oxygen then passes from the anode electrode 7 , through the larger pores of the porous sheet 14 , to the metal screen set 1 . Meanwhile, additional water is wicked through some of the smaller pores of the porous sheet 14 to the anode electrode 7 for additional electrolysis.
  • the porous sheet 14 establishes a simultaneous, dual-directional flow since the smaller pores allow water to be wicked to the anode electrode 7 while the larger pores simultaneously allow oxygen to pass from the anode electrode 7 to the metal screen set 1 .
  • the porous sheet can provide the necessary support for the ion exchange membrane during high pressure gradient operation without compromising the efficiency of the electrolyzer 10 .
  • the porous sheet should be composed of an electrically conductive compound capable of being formed into a thin sheet having multiple pore sizes, of allowing simultaneous, dual-directional flow such that the passage of oxygen or hydrogen (depending upon the side of the ion exchange membrane) occurs simultaneously with the passage of water, and of supporting the ion exchange membrane under high pressure gradient conditions. Additionally, compatibility of the porous sheet with an oxygen and water or hydrogen and water environment is important.
  • this porous sheet is a metal or an electrically conductive compound such as carbon, niobium, tantalum, titanium, zirconium, mixtures thereof, and others.
  • the sheet thickness can range from about 0,127 mm to about 0.635 mm with a thickness of about 0.293 mm to about 0.305 mm preferred.
  • the pore size of the porous sheet is dependent upon the size of the molecules which must pass through these pores. Pore sizes ranging from about 10 ⁇ m (microns) to about 14 ⁇ m (microns) have proven useful. Since porosities exceeding 60% tend to decrease the strength of the porous sheet and therefore its ability to provide structural integrity to the ion exchange membrane, and since porosities below about 40% inhibit the flow of the water and oxygen or hydrogen to and from the respective electrode, the porosity of the porous sheet typically ranges from about 40% to about 60%.
  • the porous sheet electrical conductivity can be improved by electroplating it with a conductive metal.
  • a metal conventionally used to form the anode and cathode electrodes can be utilized for electroplating purposes.
  • a few of the possible electroplating metals include gold, iridium, palladium, platinum, rhodium, ruthenium, and mixtures thereof, among others, with platinum preferred.
  • the porous sheets are fine spotted using conventional electroplating techniques with about 0.05 milligrams per square centimeter (mg/cm 2 ) to about 0.2 mg/cm 2 of the electroplating metal, with about 0.07 mg/cm 2 to about 0.12 mg/cm 2 preferred.
  • porous sheets can be interposed between the anode electrode, cathode electrode, or both, and the metal screen sets, depending upon where dual-directional flow is needed and the amount of support necessary.
  • submarine electrolyzers preferably utilize the porous sheets interposed between the anode electrode and the metal screen set forming the anode chamber
  • aircraft electrolyzers preferably utilize the porous sheets interposed between the cathode electrode and the metal screen set forming the cathode chamber.
  • the ship directly receives low pressure metabolic oxygen from the electrolyzer while the hydrogen is delivered to discharge at sea depth pressure. Therefore, the ion exchange membrane cathode side pressure exceeds the anode side pressure, resulting in a pressure gradient up to about 6.89MPa (1000 psi). If the ion exchange membrane is not supported by the porous sheet, it potentially can be extruded into the metal screen set on the anode side causing ion exchange membrane and electrolyzer failure.
  • hydrogen in an aircraft 1.38 MPa (200 psi) oxygen recharge system, hydrogenat about 0,138 MPa (20 psi), reacts wit ambient air at altitude pressure (i.e. cabin pressure).
  • the ion exchange membrane anode side pressure exceeds the cathode side pressure, resulting in a pressure gradient up to about 13.8 MPa (2,000 psi). Again, the potential for ion exchange membrane failure is created without porous sheet support of the ion exchange membrane on the cathode side.
  • anode and cathode electrodes include metal and metal alloys of noble metals, such as iridium based, palladium based, platinum based, rhodium based, and ruthenium based metals, mixtures thereof, and other catalytic metals known in the art.
  • Conventional electrolyzer ion exchange membranes allow hydrogen ion migration from the anode electrode to the cathode electrode.
  • Typical long life ion exchange membranes are of the perfluorocarbon sulfonic acid type due to their electrochemical stability.
  • One such perfluorocarbon sulfonic acid membrane is Nafion® produced by E.I. duPont de Nemours & Co. (Inc.), Wilmington, Delaware. Similar perfluorocarbon sulfonic acid membranes are produced by Dow Chemical and others.
  • Conventional metal screens include screens having a thickness and a mesh size determined on the basis of mass flow rates, pressure, and temperature conditions. Typically, these metal screens have a mesh size of about 2/0 to about 6/0, with about 2/0 to about 4/0 preferred.
  • the metal screen thickness typically ranges from about 0.05 mm to about 0.5 mm, with about 0.05 mm to about 0.3 mm preferred.
  • Operation of one embodiment of the water electrolyzer of the present invention comprises introduction of water to the anode chamber.
  • the water passes through the metal screen set, through the porous sheet, and intimately contacts the anode electrode.
  • electrolysis converts the water to hydrogen ions and oxygen.
  • the hydrogen ions migrate across the ion exchange membrane to the cathode electrode, form molecular hydrogen at the cathode electrode, and exit the electrolyzer through the cathode chamber as molecular hydrogen.
  • the oxygen passes from the anode electrode through the larger pores in the porous sheet, through the metal screen set, and exits the electrolyzer as additional water simultaneously passes through the metal screen set and through the porous sheet to the anode electrode.
  • one or a plurality of porous sheets can be utilized on one or both sides of the ion exchange membrane depending upon where and the amount of support required.
  • one or a plurality of fine screens can be used with one or a plurality of porous sheets on the respective sides of the ion exchange membrane. Therefore, the arrangement of the electrolyzer could be (referring to Figure 4) metal screen set 1 , porous sheet 14 , anode electrode 7 , ion exchange membrane 5 , cathode electrode 9 , fine mesh screen 12 , second metal screen set 3 . This arrangement would allow the dual-directional flow necessary for the passage of water and oxygen and also allow uni-directional flow of the hydrogen while increasing the structural integrity of both sides of the ion exchange membrane.
  • the advantages of the present invention range from improved structural integrity and the ability to successfully operate under high pressure gradient conditions to improved cell performance under all practical pressure gradient conditions.
  • These pressure gradients include gradients up to about 6000 psi and possibly greater.
  • the porous sheet electrolyzer maintained a current density below 2 volts at a higher current density and higher pressure gradient ⁇ P) than the metal screen set electrolyzer; a ⁇ P of 5.17 MPa (750 psi) and a current density of about 10753 A/m 2 (1000 ASF) at 2 volts (Line 2) versus a ⁇ P below 1.38 MPa (200 psi) and a current density below about 8925 A/m 2 (830 ASF) (Line 3), respectively.
  • fine mesh screen and the porous sheet electolyzers operated at ⁇ P of about 5,17 MPa (750 pounds per square inch (psi)) while the metal screen set electrolyzer operated below about 1.38 MPa (200 psi) ⁇ P.
  • the ion exchange membrane electrolyzer of the present invention is capable of operating at pressure gradients up to about 41.34 MPa (6,000 psi) without the use of additional equipment and without sacrificing electrolyzer performance.
  • the electrolyzer performance of the present invention is superior to that of the prior art over a wide range of pressures and current densities; from about 0.69 MPa (100 psi) to about 20.68 MPa (3,000 psi) and greater, and from about 1075 A/m 2 (100 ASF) to about 21505 A/m 2 (2,000 ASF).

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
  • Electrodes For Compound Or Non-Metal Manufacture (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
EP93914147A 1992-06-02 1993-05-25 Dual-directional flow membrane support for water electrolyzers Expired - Lifetime EP0642601B1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
US892152 1992-06-02
US07/892,152 US5296109A (en) 1992-06-02 1992-06-02 Method for electrolyzing water with dual directional membrane
PCT/US1993/004969 WO1993024677A1 (en) 1992-06-02 1993-05-25 Dual-directional flow membrane support for water electrolyzers

Publications (2)

Publication Number Publication Date
EP0642601A1 EP0642601A1 (en) 1995-03-15
EP0642601B1 true EP0642601B1 (en) 1996-11-06

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ID=25399462

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EP93914147A Expired - Lifetime EP0642601B1 (en) 1992-06-02 1993-05-25 Dual-directional flow membrane support for water electrolyzers

Country Status (6)

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US (2) US5296109A (ja)
EP (1) EP0642601B1 (ja)
JP (1) JP3264493B2 (ja)
AT (1) ATE145019T1 (ja)
DE (1) DE69305850T2 (ja)
WO (1) WO1993024677A1 (ja)

Families Citing this family (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5521023A (en) * 1990-08-16 1996-05-28 Kejha; Joseph B. Composite electrolytes for electrochemical devices
US5342494A (en) * 1993-03-05 1994-08-30 United Technologies Corporation High purity hydrogen and oxygen production and apparatus therefor
JP3400508B2 (ja) * 1993-10-27 2003-04-28 ペルメレック電極株式会社 塩水電解方法及び電解槽
US5686051A (en) * 1994-11-11 1997-11-11 Kabushiki Kaisha Kobe Seiko Sho Ozone water production apparatus
JP3213213B2 (ja) * 1995-09-06 2001-10-02 ホシザキ電機株式会社 電解槽
DE19544585C1 (de) * 1995-11-30 1997-06-26 Dornier Gmbh Elektrolyseur mit flüssigem Elektrolyten
WO1997044838A1 (en) * 1996-05-24 1997-11-27 Lithium Technology Corporation Composite electrolytes for electrochemical devices
US6037075A (en) * 1996-11-26 2000-03-14 United Technologies Corporation Electrically non-conductive plate structures and high pressure electrochemical cell devices employing same
US6576096B1 (en) 1998-01-05 2003-06-10 Lynntech International, Ltd. Generation and delivery device for ozone gas and ozone dissolved in water
US6024848A (en) * 1998-04-15 2000-02-15 International Fuel Cells, Corporation Electrochemical cell with a porous support plate
US6117287A (en) * 1998-05-26 2000-09-12 Proton Energy Systems, Inc. Electrochemical cell frame
EP1112229A4 (en) 1998-05-29 2004-06-16 Proton Energy Systems LIQUID CONTROL SYSTEM FOR VAN WATER ELECTROLYSIS
JP2002519508A (ja) * 1998-06-22 2002-07-02 プロートン エネルギー システムズ．インク 電気化学電池用のスクリーンアセンブリ
EP1147243B1 (en) * 1998-12-29 2003-11-19 Proton Energy Systems, Inc. Integral screen/frame assembly for an electrochemical cell
US6270636B1 (en) 1998-12-31 2001-08-07 Proton Energy Systems, Inc. Integrated membrane and electrode support screen and protector ring for an electrochemical cell
DE19916240B4 (de) * 1999-04-10 2004-05-06 H2-Interpower Brennstoffzellensysteme Gmbh I.Ins. Hydrolyseur
KR20020074451A (ko) * 1999-11-18 2002-09-30 프로톤 에너지 시스템즈, 인코포레이티드 높은 압력 차이 전기화학 전지
US7153409B2 (en) * 1999-12-16 2006-12-26 Proton Energy Systems, Inc. Electrochemical cell system and method of operation
WO2001045192A1 (en) 1999-12-16 2001-06-21 Proton Energy Systems, Inc. Low gravity electrochemical cell
US6860976B2 (en) * 2000-06-20 2005-03-01 Lynntech International, Ltd. Electrochemical apparatus with retractable electrode
KR100913852B1 (ko) * 2000-12-12 2009-08-26 테르사노 아이엔씨. 오존수를 생성하고 적용하기 위한 장치 및 방법
US20030196893A1 (en) * 2002-04-23 2003-10-23 Mcelroy James Frederick High-temperature low-hydration ion exchange membrane electrochemical cell
WO2003103082A2 (en) 2002-05-31 2003-12-11 Lynntech, Inc. Electrochemical cell and bipolar assembly for an electrochemical cell
WO2004015805A2 (en) * 2002-08-09 2004-02-19 Proton Energy Systems, Inc. Electrochemical cell support structure
US20040060867A1 (en) * 2002-09-27 2004-04-01 Bmc Industries, Inc. Membrane support devices and methods of manufacturing
US7217472B2 (en) * 2003-12-18 2007-05-15 Hamilton Sundstrand Corporation Electrolyte support member for high differential pressure electrochemical cell
US7935456B2 (en) * 2005-09-13 2011-05-03 Andrei Leonida Fluid conduit for an electrochemical cell and method of assembling the same
WO2007051010A2 (en) * 2005-10-28 2007-05-03 Andrei Leonida Fuel cell system suitable for complex fuels and a method of operation of the same
GB0605393D0 (en) * 2006-03-16 2006-04-26 Itm Fuel Cells Ltd Composite menbranes for electrochemical cells
US7648616B1 (en) * 2006-03-31 2010-01-19 Lam Research Corporation Apparatus and method for semiconductor wafer electroplanarization
US20080199774A1 (en) * 2007-02-20 2008-08-21 Commonwealth Scientific And Industrial Research Organisation Membrane electrode assembly with electrode support
GB0801268D0 (en) * 2008-01-24 2008-02-27 Itm Power Research Ltd Improvements to electrolysis
JP5054049B2 (ja) * 2009-02-18 2012-10-24 本田技研工業株式会社 電解装置
US20100276278A1 (en) * 2009-04-30 2010-11-04 Doug Bender Modular electrolysis device
US8524028B2 (en) 2009-08-25 2013-09-03 Hamilton Sundstrnad Space Systems International, Inc. Laminate assembly sealing method and arrangement
KR101072813B1 (ko) * 2009-09-02 2011-10-14 (주)아쿠아테크 전극 분리식 연수기
US20110198232A1 (en) * 2010-02-15 2011-08-18 Hamilton Sundstrand Corporation High-differential-pressure water electrolysis cell and method of operation
JP5232271B2 (ja) * 2010-09-24 2013-07-10 本田技研工業株式会社 高圧水電解装置

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3379634A (en) * 1965-05-24 1968-04-23 Air Force Usa Zero gravity electrolysis apparatus
CH640005A5 (de) * 1979-01-17 1983-12-15 Bbc Brown Boveri & Cie Elektrolysezelle fuer die wasserzersetzung.
DE2927566C2 (de) * 1979-07-07 1986-08-21 Kernforschungsanlage Jülich GmbH, 5170 Jülich Diaphragma für alkalische Elektrolyse, Verfahren zur Herstellung desselben und dessen Verwendung
JPS5693883A (en) * 1979-12-27 1981-07-29 Permelec Electrode Ltd Electrolytic apparatus using solid polymer electrolyte diaphragm and preparation thereof
US4331523A (en) * 1980-03-31 1982-05-25 Showa Denko Kk Method for electrolyzing water or aqueous solutions
DE3132947A1 (de) * 1981-08-20 1983-03-03 Uhde Gmbh, 4600 Dortmund Elektrolysezelle
IL67047A0 (en) * 1981-10-28 1983-02-23 Eltech Systems Corp Narrow gap electrolytic cells
US4414092A (en) * 1982-04-15 1983-11-08 Lu Wen Tong P Sandwich-type electrode
US4715938A (en) * 1986-03-27 1987-12-29 Billings Roger E Method and apparatus for electrolyzing water
US4950371A (en) * 1989-03-24 1990-08-21 United Technologies Corporation Electrochemical hydrogen separator system for zero gravity water electrolysis

Also Published As

Publication number Publication date
DE69305850T2 (de) 1997-03-06
US5296109A (en) 1994-03-22
WO1993024677A1 (en) 1993-12-09
EP0642601A1 (en) 1995-03-15
JPH10512922A (ja) 1998-12-08
ATE145019T1 (de) 1996-11-15
DE69305850D1 (de) 1996-12-12
JP3264493B2 (ja) 2002-03-11
US5372689A (en) 1994-12-13

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